Integrated energy and/or synthesis gas production method by in-situ oxygen production, chemical looping combustion and gasification

Abstract

The invention relates to an integrated method of in-situ oxygen production, chemical looping combustion and gasification of liquid, solid or gaseous fuels allowing combustion of coal, petroleum coke and/or liquid hydrocarbons and notably heavy and/or extra heavy or bituminous residues for production of synthesis gas under pressure and/or energy.

The invention claimed is: 
     
       1. A method of producing energy and/or synthesis gas through gasification of at least one liquid and/or solid feed in at least one chemical loop comprising at least four distinct oxidation, reduction, gasification and oxygen production reaction zones, wherein:
 a) oxygen is produced in an oxygen production reaction zone R 2  by exposing an oxygen carrier solid comprising a metallic oxide, in its state of maximum oxidation, to a gaseous atmosphere with a low oxygen partial pressure comprising a carrier gas comprising reduction effluents; 
 b) the oxygen produced in stage a) is transported by means of the carrier gas to a gasification reaction zone R 4  and gasification of the liquid and/or solid feed is carried out by contacting said oxygen-enriched carrier gas at high temperature with said feed so as to produce synthesis gas CO+H 2 ; 
 c) reduction of the oxygen carrier solid is carried out so as to release oxygen allowing to oxidize the synthesis gas, in a reduction reaction zone R 3 , the reduction reaction in said reduction reaction zone being exothermic; 
 d) the oxygen carrier solid that has been at least partly reduced to provide the system with oxygen is oxidized on contact with air so as to recover its maximum oxidation state, in an oxidation reaction zone R 1 , 
 
       and wherein the heat provided by the reactions involved in said oxidation reaction zone R 1  and in said reduction reaction zone R 3  is used to allow energetic operation of the method. 
     
     
       2. A method as claimed in  claim 1 , wherein the synthesis gas is produced under pressure in stage b) and expansion of the gas produced is carried out prior to reduction of the oxygen carrier solid in stage c). 
     
     
       3. A method as claimed in  claim 1 , wherein at least part of the synthesis gas produced is used in the method to provide the heat required for operation and possibly to produce excess heat that can be upgraded. 
     
     
       4. A method as claimed in  claim 3 , wherein at least part of the synthesis gas is sent to the reduction reaction zone. 
     
     
       5. A method as claimed in  claim 4 , wherein all of the synthesis gas is sent to the reduction reaction zone. 
     
     
       6. A method as claimed in  claim 1 , wherein at least part of the synthesis gas produced is upgraded at the outlet of the gasification reaction zone. 
     
     
       7. A method as claimed in  claim 1 , wherein the liquid and/or solid feed is selected from among coal, petroleum coke or liquid feeds less than 10% of which has a boiling point temperature below 340° C. 
     
     
       8. A method as claimed in  claim 1 , wherein the reduction, oxidation and oxygen production reaction zones are distinct reaction zones located in a single reactor. 
     
     
       9. A method as claimed in  claim 8 , wherein the reactor is a rotary reactor. 
     
     
       10. A method as claimed in  claim 1 , wherein the reduction, oxidation and oxygen production reaction zones are located in distinct reactors. 
     
     
       11. A method as claimed in  claim 1 , wherein the exportable excess energy is recovered by heat exchange inside the reaction zones or on the gaseous effluents. 
     
     
       12. A method as claimed in  claim 1 , wherein:
 the metallic oxide remaining transfer capacity fraction X ranges between 0.8 and 1 at the outlet of oxidation reaction zone R 1 ; 
 the remaining transfer capacity fraction X ranges between 0 and 0.3 at the outlet of reduction reaction zone R 3 ; 
 the total transfer capacity fraction ΔX ranges between 0.01 and 1 in oxygen production zone R 2 . 
 
     
     
       13. A method as claimed in  claim 12 , wherein:
 the metallic oxide remaining transfer capacity fraction X ranges between 0.95 and 1 at the outlet of oxidation reaction zone R 1 ; 
 the remaining transfer capacity fraction X ranges between 0 and 0.1 at the outlet of reduction reaction zone R 3 ; 
 the total transfer capacity fraction ΔX ranges between 0.05 and 0.5 in oxygen production zone R 2 . 
 
     
     
       14. A method as claimed in  claim 1 , further comprising recovering exportable excess energy for the production of heat. 
     
     
       15. A method as claimed in  claim 1 , further comprising upgrading at least part of the synthesis gas at the outlet of the gasification reaction zone to produce synthesis gas under pressure.